Process for polymerization of isoolefins and multiolefins

ABSTRACT

The present invention relates to an improved solution process for the formation of substantially gel-free copolymers and terpolymers of isobutylene and one or more dienes having an Mn of about less than 500,000, a mole % unsaturation of about 8 to about 45, and a polydispersity value of about 3 to about 30, wherein the mixture of isobutylene and diene monomers and a cosolvent are contacted with a catalyst at polymerization conditions (-50° -to 100° C.) wherein the improvement includes a hydrocarbon soluble catalyst being formed from the reaction product of a material of the formula: 
     
         R.sub.m AlX.sub.3-m 
    
     wherein m is an integer of from 1 to 3 inclusive, R is the same or different alkyl radical of straight or branched chain structure of from 1 to 7 carbons and X is the same or different halogen selected from the group consisting of chlorine and bromine, and a halogen containing material which is Y moles of halogen, halogen acid, or mixed halogen per mole of aluminum compound wherein the halogen is selected from the group consisting of chlorine and bromine, wherein the molar ratio of the formed catalyst to the monomer is critical by selecting at about 0.0001 to about 0.001 in order to obtain the desired elastomeric co- and terpolymers. The molar ratio of the halogen containing material to the R m  Al 3-m  used in forming the catalyst is critically selected at about 0.014 to about 0.065. This improved process permits the formation of high quality elastomeric products at improved polydispersity levels and higher monomer conversions.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to an improved solution process for the formation of gel-free copolymers and terpolymers of isobutylene and one or more dienes having an Mn of about less than 500,000, a mole % unsaturation of about 8 to about 45, and a polydispersity value of about 3 to about 30, wherein the mixture of isobutylene and diene monomers and a cosolvent are contacted with a catalyst at polymerization conditions (-50° to -100° C.) wherein the improvement includes a hydrocarbon soluble catalyst being formed from the reaction product of a material of the formula:

    R.sub.m AlX.sub.3-m

wherein m is an integer of from 1 to 3 inclusive, R is the same or different alkyl radical of straight or branched chain structure of from 1 to 7 carbons and X is the same or different halogen selected from the group consisting of chlorine and bromine, and a halogen containing material which is Y moles of halogen, halogen acid, or mixed halogen per mole of aluminum compound wherein the halogen is selected from the group consisting of chlorine and bromine wherein the molar ratio of the formed catalyst to the monomer is critical by selecting at about 0.0001 to about 0.001 in order to obtain the desired elastomeric co- and terpolymers. The molar ratio of the halogen containing material to the R_(m) Al_(3-m) used in forming the catalyst is critically selected at about 0.014 to about 0.065. This improved process permits the formation of high quality elastomeric products at improved polydispersity levels and higher % conversions.

2. Description of the Prior Art

Aluminum compounds are widely used as polymerization catalysts. Aluminum chloride is commonly used to initiate cationic polymerizations but it has the disadvantage of little or no solubility in many desirable hydrocarbon systems especially where homogeneous polymerizations are required. Aluminum bromide which is soluble in hydrocarbons, has limited utility as such in a number of desirable systems. Alkylaluminum dihalides are generally less reactive than the aluminum halides but offer the advantage of excellent hydrocarbon solubility. To enhance their reactivity, they are frequently used together with cocatalysts. Proton donators like the halogen acids, are placed in the polymerization medium and are said to be ionized by the aluminum compound thereby releasing protons to initiate polymerization. Halogens and organic halogen compounds are also ionized in situ to initiate cationic polymerization. In the case of dialkylaluminum halides and aluminum alkyls, such cocatalysts are required since these compounds are not generally active in themselves. Also compounds like dialkylaluminum iodides and alkylaluminum diiodides, which are generally not effective initiators in and of themselves, have been utilized with halogen cocatalysts, such as iodine, to initiate the polymerization. The iodine must be present in the polymerization medium and is ionized by the aluminum component, the ions initiating the polymerization. This is a good illustration of cocatalysis since neither the starting alkylaluminum iodides nor the product aluminum iodide is a catalyst by itself so the co-catalyst must be present in the polymerization medium.

The catalyst systems of the instant invention differ markedly from those of the prior art. The halogens, halogen acids, interhalogen compounds and organic halogen compounds are not used as cocatalysts but instead are prereacted with the organic aluminum compound to generate novel catalyst species which are hydrocarbon soluble and can be utilized in hydrocarbon polymerization systems. These catalysts are generally more reactive and give higher molecular weights than the corresponding organoaluminum compounds from which they are derived. Furthermore, the prereacted catalysts of the instant invention give products superior to the polymerization products obtained using halogens, halogen acids, interhalogen compounds or organic halides as cocatalysts.

Numerous prior art examples using cocatalysts are extant. These are clearly distinguishable from the catalysts of the instant invention. The halides, etc. of the prior art are used either in situ as cocatalysts or as complexing agents.

U.S. Pat. No. 2,220,930 teaches the manufacture of polymers using catalysts such as dialkylaluminum halides or alkylaluminum halides, generally represented as MX_(m) R_(n) where M represents aluminum, gallium or boron, X represents halogen, R represents a monovalent hydrocarbon radical, m or n represent integers 1 to 2 inclusive, and M+n=3. The catalyst can also be a complex of the above compounds with inorganic halides (e.g. NaCl) or with ammonia or amines. In practice, U.S. Pat. No. 2,220,930 utilized either dialkylaluminum halides or alkylaluminum dihalides alone or in a mixture of equal parts which is commonly known as the sesquihalide. The polymers of isobutylenes obtained were low molecular weight resins.

U.S. Pat. No. 2,387,517 relates to the manufacture of polymers prepared by the copolymerization of various unsaturated compounds in the presence of catalysts of the type MX_(m) R_(n) where M represents aluminum, gallium, or boron, X represents a halogen, R represents a monovalent hydrocarbon radical, m or n represent integers from 1 to 2 inclusive and m+n=3. The invention is particularly directed to the formation of curable rubber-like products by the copolymerization of isobutylene with low molecular weight diolefins, especially those having 4 to 6 carbon atoms. The products are described as ranging in molecular weight from 1000 to 3000 up to 300,000 or higher. However, the type of molecular weight is not indicated (most likely viscosity average molecular weight) nor is an actual polymer approaching 300,000 molecular weight prepared. The composition used as catalysts in the above two related cases are not prepared by prereacting an alkyl aluminum halide with halogens, halogen acid or interhalogen compounds of the instant invention and do not suggest, the superiority which the instant compositions demonstrate as catalysts.

U.S. Pat. No. 2,388,428 relates to an improved method for affecting organic chemical reactions by generating Friedel-Crafts metal halide catalysts in situ. It teaches dissolving an organo aluminum compound in a hydrocarbon reactant being charged to the process and contacting said solution with an excess of hydrogen halide in a reaction zone under hydrocarbon conversion conditions whereby an aluminum halide catalyst is generated in situ and the conversion reaction is affected. The hydrogen halide is added in excess (in an excess over the amount required to completely convert the organoaluminum compound to the aluminum halide so as to generate aluminum halide (e.g., AlCl₃) in situ). Such generation of aluminum chloride is described as being subject to greater control and of greater precision than prior art methods of dissolving or suspending the aluminum halide in the reaction mixture. Particular note should be taken of the fact that the catalyst components are not prereacted and then added to the reaction zone, but are reached in situ. Furthermore, the stoichiometry is quite different from the catalysts of the instant invention. The molar ratio of catalyst to monomer is greater than 0.026 and the cocatalyst to catalyst ratio is greater than 4.4. The use of the catalyst of U.S. Pat. No. 2,388,428 for the purposes of polymerization is not taught as the examples are directed solely to isomerization and alkylation at temperatures of 10° C. to 77° C.

U.S. Pat. No. 3,349,065 teaches an improved catalyst system for producing high molecular weight butyl rubbers having less than 5.5% mole unsaturation by a slurry process which are highly gelled (4.7 to 70%). The catalyst system comprises a dialkylaluminum halide together with a small but critical amount of an anhydrous hydrogen halide as a promoter (cocatalyst). The amount of anhydrous hydrogen halides used ranges from 0.01 mole to 0.05 mole promoter per mole of dialkylaluminum monohalide. The maximum desirable ratio is 0.05 mole promoter per mole of catalyst. Furthermore, the hydrogen halide is added to a solution containing both the dialkylaluminum chloride and monomer and is not prereacted with said organoaluminum compound as in the method of the instant invention. This patent does not teach, imply or infer the use of a solution process for the formation of gel-free elastomers.

U.S. Pat. No. 3,562,804 also describes the use of an organoaluminum compound in conjunction with hydrogen chloride or a C₃ -C₇ organic halide compound as promoter to produce low viscosity mastic compositions by a slurry process. Here again, the catalyst and promoter were combined in the presence of monomer and all examples teach the separate addition of catalyst and promoter to the polymerization (monomer) mixture. The catalyst to monomer ratio is at least about 0.001 and the rate of cocatalyst to catalyst is greater than about 3.0.

U.S. Pat. No. 3,850,897 teaches a procedure of the production of polymers and copolymers of isobutylene. The catalyst disclosed is of the general formula RAl(YR')X where Y is an oxygen or sulfur atom together with a wide variety of promoters. The aluminum compounds disclosed in this patent are different from those of the instant invention. Furthermore, the patent in question teaches the necessity of combining catalyst and cocatalyst in the presence of monomers. Stepwise addition of catalyst and cocatalyst to the polymerization medium is demonstrated in the examples. The catalyst to monomer ratio is at least about 0.0038.

U.S. Pat. No. 3,835,079 teaches hot melt compositions comprising styrene, isobutylene copolymer wax and a primary resin. The catalysts employed a system utilizing a primary component alkylaluminum dihalide with a promoter (cocatalyst) such as hydrogen halide. The maximum cocatalyst is 30 mole percent of the primary catalyst. A more limited range, 2.5 to 15 is preferred or 5 to 10% with cocatalysts such as water. The range of compositions is clearly outside that of the instant invention. Furthermore, the promoters are stated to be cocatalysts in this patent while they are consumed in a prior reaction in the instant invention and are not available to serve as cocatalysts.

U.S. Pat. No. 3,560,458 teaches a polymerization process utilizing a catalyst of the type Al(M)₂ R where M is an alkyl group and R is alkyl, hydrogen or halogen. It is obvious that the catalyst intended for use is the alkyl or the monohalide. Experimental procedure reveals a stepwise addition of cocatalyst promoters to a solution containing catalyst in the cationically polymerizable monomer. The molar ratio catalyst to monomer is at least about 0.007.

British Pat. No. 1,362,295 teaches a catalyst suitable for use in the polymerization of unsaturated compounds and a process for employing such a catalyst. The catalyst used is a two-component substance, the primary component being R₂ AlX wherein R is a hydrocarbon or hydrogen radical, X can be hydrocarbon, hydrogen or halogen. The secondary component is represented as YZ wherein each of Y and Z are the same or different halogen. The component can be present in a ratio of primary to secondary of from 0.1:1 to 1000:1.

Other patents which are non-applicable to the instant invention are: U.S. Pat. Nos. 3,757,000 and 3,560,458; British Pat. Nos. 1,309,131 and 1,157,043; and U.S. Pat. applications Nos. 635,695 and 737.917.

All examples contain active cocatalysts, and no criticality for prereaction of components is taught. Furthermore, the ratios of materials involved are such as to not practice the invention of the instant specification and no showing is made of there being a ratio demonstrating superior performance.

SUMMARY OF THE INVENTION

The present invention relates to an improved solution process for the formation of substantially gel-free copolymers and terpolymers of isobutylene and one or more dienes having an Mn of about less than 500,000, a mole % unsaturation of about 8 to about 45, and a polydispersity value of about 3 to about 30, wherein the mixture of isobutylene and diene monomers and a cosolvent are contacted with a catalyst at polymerization conditions (-50° to -100° C.) wherein the improvement includes a hydrocarbon soluble catalyst being formed from the reaction product of a material of the formula:

    R.sub.m AlX.sub.3-m

wherein m is an integer of from 1 to 3 inclusive, R is the same or different alkyl radical of straight or branched chain structure of from 1 to 7 carbons and X is the same or different halogen selected from the group consisting of chlorine and bromine, and a halogen containing material which is Y moles of halogen, halogen acid, or mixed halogen per mole of aluminum compound wherein the halogen is selected from the group consisting of chlorine and bromine wherein the molar ratio of the formed catalyst to the monomer is critical by selecting at about 0.0001 to about 0.001 in order to obtain the desired elastomeric co- and terpolymers. The molar ratio of the halogen containing material to the R_(m) Al_(3-m) used in forming the catalyst is critically selected at about 0.014 to about 0.065.

Accordingly, it is an object of the instant invention to provide an improved solution process for the formation of high quality, substantially gel-free elastomers of co- and terpolymers of isobutylene and one or more dienes having an Mn of less than about 500,000, a mole % unsaturation of about 8 to about 45, and a polydispersity of about 3 to about 30. The process includes the formation of a catalyst from the reaction ratio of R_(m) AlX_(3-m) and a halogen containing material at a molar ratio of the halogen containing material to the R_(m) AlX_(3-m) of about 0.014 to about 0.065 and the subsequent use of the formed catalyst at a molar ratio of catalyst to monomer of about 0.0001 to about 0.001, wherein improved monomer conversion at higher polymerization temperatures are readily attainable thereby improving the efficiency of the process. The process is further improved economically by reduction of the ratio of isobutylene to cosolvent thereby resulting in higher monomer % conversion as well as increase cement concentration.

GENERAL DESCRIPTION

The novel halogenated organoaluminum catalysts employed in the improved process of the instant invention are prepared by reacting a material of the formula R_(m) AlX_(3-m) wherein m is from 1 to 3, R is an alkyl radical of straight or branched chain structure of from 1 to 7 carbons and X is the same or different halogen selected from the group consisting of chlorine and bromine and a halogen containing material which Y moles of a halogen, halogen acid, or mixed halogen per mole of aluminum compound wherein the halogen is selected from the group consisting of chlorine and bromine.

In a more particular embodiment, novel organoaluminum catalysts are prepared by reacting a material of the formula RAlX₂ wherein R is an alkyl radical of straight or branched chain structure of from 1 to 7 carbons and X is the same or different halogen selected from the group consisting of chlorine and bromine with the halogen containing material which is Y moles of a halogen, halogen acid, or mixed halogen wherein the halogen is selected from the group consisting of chlorine and bromine.

In an alternative embodiment, the novel catalysts are prepared by mixing materials of the formula R₂ AlX wherein R is the same or different alkyl radical of straight or branched chain structure of from 1-7 carbons and X is a halogen selected from the group consisting of chlorine and bromine with the halogen containing material which is Y moles of a halogen, halogen acid, or mixed halogen per mole of dialkyl aluminum monohalide wherein the halogen is selected from the group consisting of chlorine and bromine.

In yet another embodiment, the novel catalysts are prepared by mixing, before use, materials of the formula R₃ Al, wherein R is the same or different alkyl radical of straight or branched chain structure of from 1-7 carbons with the halogen containing material which is Y moles of halogen, halogen acid, or mixed halogen per mole of trialkyl aluminum compound, wherein the halogen is selected from the group consisting of chlorine and bromine.

The catalyst preparation is preferably carried out in a solvent, more preferably in a hydrocarbon solvent, most preferably in a paraffinic hydrocarbon liquid or mixtures thereof, of from 1 to 10 carbons which may be normal, branched or cyclic in structure. The components are preferably diluted in an inert paraffinic solvent such as butane, isobutane, pentane, isopentane, hexane, isomeric hexanes, cyclohexane, methylcyclohexane or mixtures of paraffinic solvents are the solvents of choice for the polymerization so as to facilitate mixing and reaction. The catalyst solution concentrations may range from 0.01 to 50%, preferably 0.2 to 20%, e.g. 1%.

The molar ratio of the R_(m) AlX_(3-m) to the monomer is about 0.0001 to about 0.001, more preferably about 0.0002 to about 0.0008, and most preferably about 0.0004 to about 0.0006. The molar ratio of halogen containing material to R_(m) Al_(3-m) is critically selected at about 0.014 to about 0.065, more preferably at about 0.025 to about 0.055 and most preferably about 0.030 to about 0.050. The formation of the catalyst is done prior to contact with the monomers and is preferably at least about 60 seconds, more preferably about 20, and most preferably about 5 thereby ensuring formation of the catalyst prior to contact with the monomers and thus minimizing adverse side reactions of either the halogen containing material.

The reactive catalyst entity thus prepared, exhibits higher catalytic activity and efficiency than catalysts of the prior art and permits polymerization reactions to be run which yield higher molecular weight polymers and copolymers at higher temperature and/or the inclusion of a greater degree of unsaturation in a polymer of either high or low molecular weight at temperatures higher than previously possible.

The compounds of this invention are particularly beneficial for homogeneous cationic solution polymerization in hydrocarbon media since they are more reactive than alkylaluminum dichlorides or dibromides alone. They also avoid difficulties associated with using hydrocarbon insoluble catalysts such as AlCl₃ since hydrocarbon slurries of the latter frequently cause gelation or fouling, while using polar solvent (i.e. methyl chloride) solutions of the latter catalyst require counteracting the effects of the polar catalyst solvent which is a nonsolvent for the polymer and require diluting the monomer with additional quantities of polymer solvent to maintain homogeneous polymerization conditions.

The catalysts of this invention offer further benefits in that they frequently give higher molecular weight polymers and copolymers than the generally available organoaluminum compounds from which they are conveniently and inexpensively prepared. The formation of polymers of higher molecular weights with the novel catalysts of this invention frequently permits operation at warmer polymerization temperatures (-50° to -100° C.) while yielding equivalently high molecular weight polymers. Since polymer molecular weights generally decrease with increasing temperature in prior art cationic polymerizations, the ability of the instant invention to yield high molecular wt. polymers at higher temperature is a marked advance over the prior art. Since polymerizations are generally quite exothermic and frequently carried out at low temperatures, process limitations relating to solution viscosity, heat transfer rates, maximum solids contents and ultimately production capacity for a given size unit are encountered. Thus, it is beneficial and industrially quite valuable if the desired molecular weights can be attained at warmer polymerizations temperatures. The present invention features these characteristics and advantages.

The catalysts of this invention are particularly valuable since they not only give high catalyst efficiencies and high monomer % conversion but they also produce higher molecular weight polymers, copolymers at warmer temperatures than conventional catalysts.

One group of cationically polymerizable monomers suitable for use with the novel catalysts of the instant invention are cationically polymerizable unsaturated compounds, especially unsaturated hydrocarbons. Particularly valuable polymers can be prepared from isoolefins, of from 4 to 20 carbons, multiolefins of from 5 to 20 carbons, or mixtures thereof to produce homopolymers and copolymers. Examples of such unsaturated hydrocarbons include but are not restricted to isobutylene, 2-methylbutene, 3-methyl-butene-1,4-methylpentene-1, and β-pinene. Multiolefins include but are not limited to butadiene, isoprene, piperylene, 2,3-dimethylbutadiene, cyclopentadiene, methyl cyclopentadiene, 1,3-cyclohexadiene, dimethylfulvene and divinylbenzene.

The compounds of this invention are prepared by reacting in an inert solvent, preferably a hydrocarbon solvent, more preferably a paraffinic hydrocarbon solvent, most preferably a paraffinic solvent C₁ -C₁₀, a hydrocarbyl aluminum halide compound together with a halogen, interhalogen, or halogen acid. The hydrocarbyl aluminum compound has the general formula R_(m) AlX_(3-m) wherein R is a hydrocarbyl group, preferably an alkyl group up to C₇, most preferably, a C₁ to C₄ alkyl group and X is a halogen or mixture of halogens, preferably chlorine or bromine, most preferably, chlorine and m is 1-3 inclusive. Preferably, the hydrocarbyl aluminum halide compound has m=1. Most preferably, the hydrocarbyl aluminum halide compound is an alkyl aluminum dichloride.

The quantity halogen containing materials selected from the group consisting of halogen, halogen acid, or mixed halogen which must be reacted with the hydrocarbyl aluminum compound to obtain the desired catalyst is determined by the value of m in the hydrocarbyl aluminum compound. The molar ratio of the halogen containing material to RAlX₂ is about 0.014 to about 0.065, more preferably about 0.025 to about 0.055 and most preferably about 0.030 to about 0.050. The molar ratio of halogen containing material to R₂ AlX is about 0.030 to about 0.090, more preferably about 0.040 to about 0.080 and most preferably 0.050 to about 0.070. The molar ratio of halogen containing material to R₃ Al is about 0.040 to about 0.12, more preferably about 0.050 to about 0.11.

It is a vital requirement of this invention that said aluminum compound be reacted with said halogen, halogen acid or mixed halogen compound sufficiently prior to introducing the resultant catalyst solution into a polymerization feed containing monomers and cosolvent so as to insure reaction between the catalyst component species. The cosolvents of the instant invention are selected from the group consisting of cyclic, branched or normal paraffinic hydrocarbons, and mixtures thereof. A preferred cosolvent system is a blend of 75 wt. % of cyclohexane and 25% wt. % hexane. The weight ratio of isobutylene to cosolvent is critically selected at about 1 to about 10, more preferably at about 1.5 to about 6 and most preferably at about 2 to about 5. The critical selection of the ratio of isobutylene to cosolvent provides increased monomer % conversion at increased cement concentration thereby making the process more economical. The operating temperature of polymerization is about -50° to about -100° C., more preferably about -60° to about -95° and most preferably about -70° to about -90°. The operating pressure is about 0 to about 1000 psig, more preferably about 5 to about 500, and most preferably about 15 to about 300 and the nominal residence time in a continuous process is about 1 to about 60 minutes, more preferably about 5 to about 30 and most preferably about 10 to about 20.

The components used in forming the catalyst must be premixed, preferably at least 60 seconds, more preferably 20 seconds, most preferably 5 seconds before use. The halogen, halogen acid or mixed halogen compound may be admixed with a solution of hydrocarbylaluminum dihalide either as neat liquids, gases or preferably in solution in an inert solvent. Solvents such as paraffins are inert to halogens in the absence of free radical initiators and radiation, therefore, said solutions should be protected from light prior to the reaction with aluminum compound. It is absolutely essential that the components be premixed prior to use.

One embodiment of this invention is the utilization of said novel catalysts in improved processes for the preparation of isoolefin homopolymers and copolymers of an isoolefin with multiolefins or mixtures of multiolefins. These catalysts have been found to be surprisingly useful for the production of valuable highly unsaturated high molecular weight copolymer of isobutylene with conjugated diolefin(s). Some of the characteristics of these processes are higher catalyst efficiencies and higher polymer molecular weights than are realized with ordinary hydrocarbylaluminum dihalides. Many of the novel catalysts of this invention are soluble in hydrocarbons even paraffinic hydrocarbons. They are active in an all hydrocarbon system of monomers and solvents (cosolvents) and frequently give greater monomer conversions, more rapid polymerization, and higher molecular weights. Thus under a wide variety of conditions these catalysts achieve faster reactions and higher molecular weights at warmer temperatures than conventional hydrocarbyl aluminum dihalide catalysts. These catalysts are particularly valuable for the production of extraordinarily high molecular weight highly unsaturated copolymers of isobutylene and conjugated diolefins such as cyclopentadiene. As a consequence, highly unsaturated copolymers with number average molecular weights similar to those obtained with hydrocarbylaluminum dihalide can be produced at substantially warmer polymerization temperatures.

The Mn of the co- or terpolymers formed by the unique and novel process of the instant invention are about 30,000 to about 500,000, more preferably about 40,000 to about 400,000, and most preferably about 50,000 to about 300,000, wherein the mole % unsaturation is about 8 to about 45, more preferably about 10 to about 40, and most preferably about 12 to about 40.

Some examples which follow will illustrate some aspects of the utility of the new improved process. It is emphasized that these examples are illustrative and other applications will be obvious to those skilled in the art.

EXAMPLE I

A series of copolymers were prepared according to this invention by the following procedure:

All feed streams were dried before they were injected into a well-stirred stainless steel reactor. The first stream consisted of 75.7 wt. % isobutylene, 7.6 wt. % cyclopentadiene (CPD) and 15.9 wt. % cosolvent (75 wt. % cyclohexane and 25 wt. % hexane). The second feed stream consisted of ethylaluminumdichloride which was dissolved in cosolvent and anhydrous hydrogen chloride.

The first feed stream was chilled to a temperature of -131° C. prior its continuous introduction into the reactor. The second (catalyst) stream which is ethylaluminumdichloride (EADC) and HCl entered the reactor through a separated feed nozzle at ambient temperature. The contact time of the EADC and HCl was about 5 seconds. The temperature of the reactor and its contents was maintained constant at -100° C. by circulating refrigerant through the reactor jacket. The feed rates of the isobutylene, CPD and cosolvent were adjusted so that a 11-minute nominal residence time was provided in the reactor.

Polymerization occurred only in the reactor. The reactor effluent was contacted with an isopropyl alcohol-ammonia quench stream to deactivate the catalyst.

The process conditions were the following when the reactor achieved steady state:

                  TABLE 1                                                          ______________________________________                                                          Feeds, gram/hr                                                ______________________________________                                         Isobutylene        19,000                                                      CPD                1,900                                                       Cosolvent          4,000                                                       EADC               17.0                                                        HCl                .30                                                         ______________________________________                                    

At steady state conditions the reactor effluent contained about 5.0 wt. % copolymer and about 4.0% of isobutylene and 25% of CPD introduced into the reactor was converted to polymer. The catalyst efficiency was 73.

The reactor effluent was then stabilized with IRGANOX 1010. The stabilized polymer solution was then steam stripped, and the precipitated polymer crumb was dried on a hot mill.

The obtained copolymer had the following properties:

                  TABLE 2                                                          ______________________________________                                         CPD content by R.I.     34.4 mole %                                            Mooney viscosity at 126.7° C.                                                                   67                                                     --Mn                    104,000                                                Inherent viscosity      1.06                                                   ______________________________________                                    

EXAMPLE II

To demonstrate the process advantages of the reduced isobutylene to cosolvent ratio of this invention, a series of copolymerization experiments were conducted according to the procedure of Example I. The process conditions and the results of the tests are shown in Tables III and IV below.

                  TABLE 3                                                          ______________________________________                                         Feeds, grams/hr           Ratio of                                             Run    ISO-C.sub.4 "                                                                           Cosolv.   CPD   ISO-C.sub.4 " Cosolv.                          ______________________________________                                         A      19,200   4,000     1,500 4.8                                            B      16,200   4,000     1,500 4.05                                           C      13,200   4,000     1,500 3.3                                            D      10,200   4,000     1,500 2.55                                           ______________________________________                                    

                  TABLE 4                                                          ______________________________________                                         Conversion, %  Cement Conc.                                                    Run   ISO-C.sub.4 "                                                                           CPD     wt. %      M.sub.L at 126.7° C.                  ______________________________________                                         A     4.8      28.5    5.5        45                                           B     5.7      32      6.5        52                                           C     6.7      37      7.7        66                                           D     8.2      39      9.1        74                                           ______________________________________                                    

Results in Table IV indicate that reducing the isobutylene/cosolvent weight ratio in the feed stream from about 5 to 2.5 which is done by reducing the isobutylene feed, surprisingly results in a significant increase in both (iso-C₄ " and CPD) conversions and also in the cement concentration. This makes the process economically much more attractive. In addition to the process advantages, it also results in copolymers with much higher molecular weights.

EXAMPLE III

According to the procedure of Example I, an isobutylene methylcyclopentadiene (MCPD) copolymer was prepared. The process conditions and the results of the test are summarized in Tables V and VI below.

                  TABLE 5                                                          ______________________________________                                         Res.                                                                           Time             Feeds, grams/hr                                               Min- Temp. ° C.        Co-                                              utes Feed   Coplym.  ISO-C.sub.4 "                                                                         MCPD  solv.                                                                               EADC  HCl                               ______________________________________                                         16   -134   -99      12,000 700   3,800                                                                               20    36                                ______________________________________                                    

                                      TABLE 6                                      __________________________________________________________________________                            Copolymer                                               Cement Conc.                                                                           Catalyst                                                                             Conversions, %                                                                          Composition       Inherent                              wt. %   Efficiency                                                                           ISO-C.sub.4 "                                                                       MCPD                                                                               MCPD, M %                                                                             M.sub.L at 127° C.                                                             --Mn                                                                               Visc.                                                                               --Mw/--Mn                        __________________________________________________________________________                                                   = Q                              10.8    89    10.7 71  25     49     102,000                                                                            1.24 8.7                              __________________________________________________________________________

The Q value (Mw/Mn) which is polydispersity was obtained by a gel permeation chromatography test, where the following data was also obtained Mv: 596,000, Mw: 900,000 and Mn: 104,000.

EXAMPLE IV

In order to illustrate the broad scope of this novel process, a test was made with methylaluminumdichloride (MADC) as the catalyst and at a copolymerization temperature of -75° C. according to procedure of Example I. The process conditions and the results of the test are shown in Tables 7 and 8 below.

                  TABLE 7                                                          ______________________________________                                         Res. Time                                                                               Feeds, grams/hr                                                       Minutes  ISO-C.sub.4 "                                                                           CPD     Cosolv. MADC    HCl                                  ______________________________________                                         18       12,000   1,800   2,560   30.0    .45                                  ______________________________________                                    

                                      TABLE 8                                      __________________________________________________________________________                           Copolymer                                                Cement conc.                                                                          Catalyst                                                                             Conversions, %                                                                          Composition    Inherent                                  wt. %  Efficiency                                                                           ISO-C.sub.4 "                                                                       CPD CPD, M %                                                                              M.sub.L at 127° C.                                                              Viscosity                                                                           --Mn                                 __________________________________________________________________________     12.5   68    9.5  50  40     23      0.7  51,000                               __________________________________________________________________________

The following terms are herein defined as used in the specification and claims and are as follows.

1. Rate--The rate of polymerization in grams per hour.

2. Efficiency--The catalyst efficiency was determined in terms of grams of polymer produced per grams of aluminum alkyl dihalide fed.

3. % Conversion--The percent of isobutylene and separately the percent of diene injected into the reaction vessel, which was converted into polymer product, was measured.

4. % Unsaturation Diene Content--The mole % of diene in the polymer was measured by refractive index, or NMR.

5. inherent Viscosity--The inherent viscosity of the polymer product was determined in decalin at 135° C. (ASTM)

6. m_(l) --the Mooney viscosity at 126.7° C. was determined using a large #1 rotor for 8 minutes.

7. Mn--The number average molecular weight was determined by membrane osmometry.

8. Gel Content--The percent of polymer insoluble in toluene at 100° C. One gram of polymer is dissolved in 100 ml of toluene at 100° C. and filtered through a fine mesh screen. The amount of insoluble polymer retained on the screen is dried and weighed and converted into % insoluble polymer. By substantially gel free is meant less than about 2 wt. % of polymer insolubles. 

What is claimed is:
 1. An improved solution process for preparing polymers from a mixture of monomers, said mixture consisting essentially of isoolefins and one or more multiolefins, said isoolefin being selected from the group consisting of isobutylene, 2-methylbutene, 3-methyl-butene-1,4-methyl-pentene-1 and β-pinene, said multiolefin being selected from the group consisting of isoprene, piperylene, cyclopentadiene, and methylcyclopentadiene and mixtures thereof which consists essentially of contacting said isoolefins and said multiolefins blended in a cosolvent with a catalyst at polymerization conditions of about -50° C. to about -100° C. at a pressure of about 0 to about 1000 psig for about 1 to about 60 minutes, said cosolvent consisting essentially of a cyclic, branched and normal paraffinic hydrocarbons, a weight ratio of said isoolefin to said cosolvent being about 1 to about 10, the improvement consists essentially of using a catalyst which consists essentially of a soluble reaction product formed in a solvent from the reaction of a material of the formula RAlX₂ and a halogen containing material, wherein R is the same or different alkyl radical of straight or branched chain structure having from 1 to 7 carbon atoms, and X is the same or different halogen selected from the group consisting of Cl and Br said halogen containing material is selected from the group consisting of halogen, halogen acid and mixed halogen wherein a molar ratio of said halogen containing material to said RAlX₂ is about 0.014 to about 0.065 and a molar ratio of said RAlX₂ to said mixture of said isoolefins and said multiolefins being about 0.0001 to about 0.001, said solvent is a C₁ -C₁₀ paraffinic hydrocarbon, wherein a concentration of said catalyst in said solvent is about 0.01 to about 50 wt. %, a conversion of said monomers to said polymer being about 5 to about 70%.
 2. The improved process of claim 1, wherein said polymer has a polydispersity value of about 3 to about
 30. 3. The improved process of claim 1, wherein said catalyst is formed at least about 5 seconds prior to contacting with said monomers.
 4. The improved process of claim 1, wherein said polymer has an Mn of about 50,000 to about 500,000 and a mole % unsaturation of about 8 to about
 45. 